Process for the manufacture of a 1,2-epoxide

ABSTRACT

The invention relates to a process for the manufacture of a 1,2-epoxide by catalytic oxidation of a terminal olefin with hydrogen peroxide wherein the catalytic oxidation is performed in a biphasic system comprising an organic phase and an aqueous reaction medium, wherein a water-soluble manganese complex is used as oxidation catalyst, wherein a terminal olefin is used with a solubility at 20° C. of at least 0.01 to 100 g in 1 liter water, and wherein the molar ratio of terminal olefin to hydrogen peroxide is in the range of from 1:0.1 to 1:2.

RELATED APPLICATION DATA

This application is a continuation application of co-pending U.S. patent application Ser. No. 13/056,793, with a filing date of Jan. 31, 2011, which application claims the benefit of PCT Application PCT/EP2009/004977 with an International Filing Date of Jul. 9, 2009, published as WO2010/012361, which PCT Application PCT/EP2009/004977 further claims priority to European Patent Application No. EP08075680.2 filed Aug. 1, 2008, the entire contents of both are hereby incorporated by reference.

TECHNICAL FIELD

The invention relates to a process for the manufacture of a 1,2-epoxide by catalytic oxidation of the corresponding terminal olefin using hydrogen peroxide and a manganese complex.

BACKGROUND ART

1,2-epoxides are valuable intermediates, especially when the molecule contains a second functional group. Thus, epoxides as a whole are a very important class of compounds as starting materials for polymers and as intermediates in the organic synthesis. Conventionally, these epoxides are prepared with the use of epichlorohydrin.

The catalytic oxidation of olefins by hydrogen peroxide has seen increased patent activity and has drawn quite some academic interest, although actual use of these oxidation reactions has not seen a commercial follow-up.

For instance the process for the manufacture of epichlorohydrin (“ECH”) in WO2004/048353 is carried out in a reaction medium comprising at least 75% w of organic material, causing significant isolation problems.

As mentioned above, epoxidation of terminal or electron-deficient olefins with hydrogen peroxide catalyst by manganese catalysts has been extensively described in the public art, but typically using acetonitrile as reaction medium. An example of such a paper is Tetrahedron Letters 43 (2002) 2619-2622, with turnover numbers of up to 860. In the oxidation of ethylbenzene, in Journal of Molecular Catalyst A: Chemical 185 (2002) 71-80, a mixture of acetonitrile and water is used. In Journal of Organometallic Chemistry 520 (1996) 195-200 a series of manganese complexes are explored on their catalytic behavior using different solvents. Water was not studied. A heterogenized Mn catalyst has been described in Angew. Chem. Int. Ed., 1999, 38, No. 7, using acetone and acetonitrile as solvents. In Bull. Korean Chem. Soc., 2003, Vol. 24, No. 12, 1835 the alkane oxidation catalyzed by manganese tmtacn complexes with hydrogen peroxide is described, using acetone as solvent. The oxidation of saturated hydrocarbons is described in Russian Chemical Bulletin, Vol. 47, No. 12, December 1998, 2379, using acetonitrile as solvent. The oxidation of alkanes is performed in Inorg. Chem., 2007, 26, 1315-1331 in aqueous nitrile (50%) or in acetone as solvent. The epoxidation of dec-1-ene with hydrogen peroxide in the presence of a dinuclear manganese derivative carried out in a biphasic system provided no epoxide, but in the presence of a small amount of acetonitrile yielded epoxide with a TON of 373, see Journal of Organometallic Chemistry 690 (2005) 4498-4504. In Adv. Synth. Catal. 2002, 344, 899-905 a table is provided on systems based on Mn-TACN derivatives as catalyst for oxidations of organic compounds with hydrogen peroxide. The solvent typically is acetone or acetonitrile, albeit that water has been mentioned for bleaching of stains or oxidation of phenols, which is believed to generate a wide range of products but little or no epoxides. The conclusion of this paper once again seems to be that acetonitrile as a solvent is required. From the same author, G. B. Shul'pin et al, there are a number of papers with the same conclusion on acetonitrile as solvent (Journal of Molecular Catalysis A: Chemical 222 (2004) 103-119). In the paper Inorg. Chem. 1996, 35, 6461-6465 the activity of new manganese catalysts was described towards olefin oxidation with hydrogen peroxide. Interestingly, the olefin oxidation studies showed that oxidation reactions in aqueous solutions of water-soluble olefins did not necessarily result in the corresponding epoxide. For instance, diols were produced when the corresponding epoxide was not sufficiently stable under the reaction conditions. This, however, is not problematic at all if the purpose of the reaction is to bleach stains and either discolor and/or remove contaminants from fabrics by improving their solubility. The mechanism of bleaching has in fact been further studied in Journal of Molecular Catalysis A: Chemical 251 (2006) 150-158. Thus, in alkaline aqueous solutions, typically employed in detergents, the dinuclear species used as catalyst yields lignin oxidation. Again, it should be noted that this process does not seem to be one suitable for actually producing epoxides.

A fairly early paper on the topic of epoxidation suggests the use of water as a solvent; see Tetrahedron Letter 39 (1998) 3221-3224, but all reactions are actually carried out in acetonitrile.

Whether epoxides may be manufactured in water as a solvent, and moreover in high turnover numbers therefore remains unclear.

In EP0618202 the epoxidation of olefins via certain manganese complexes is described. The method is said to include a step of recovering epoxidized olefin. According to this reference, epoxidation is best conducted in a fluid medium, especially an aqueous system. When the epoxidation is conducted in an aqueous medium, it is said that the best results are obtained on olefins with water-soluble groups such as those with carboxylate and hydroxyl units, e.g., vinylbenzoic acid, styrylacetic acid, and hexenoic acid which are all fully soluble in water. In addition to these water-soluble olefins also allyl alcohol is epoxidized using water as reaction medium. Allyl alcohol is completely miscible in water. A further listing of suitable olefins is provided, albeit that these are not the olefins to be used in an aqueous medium. The catalyst:olefin:hydrogen peroxide ratio in the examples is typically 1:100:10,000, which corresponds with the (preferred) ratio of oxidizing agent in relation to the olefin of from 500:1 to 20:1. Interestingly, no data is provided on the yield of epoxide, which rather suggests that the olefin is not only converted into the corresponding epoxide but also (or more so) in the corresponding diol, as might be expected on the basis of the academic studies reported on earlier in this specification.

From the above it is clear the industry is still looking for a commercially feasible process for the manufacture of 1,2-epoxides, in high turnover numbers and at high selectivity, meaning substantially free of byproducts such as diols. This process should also allow the use of an aqueous solvent as reaction medium, to avoid environmental and other problems related to acetonitrile and similar organic solvents. The present invention overcomes these disadvantages.

DISCLOSURE OF THE INVENTION

Accordingly, the invention provides a process for the manufacture of a 1,2-epoxide by catalytic oxidation of a terminal olefin with hydrogen peroxide wherein the catalytic oxidation is performed in a biphasic system comprising an organic phase and an aqueous reaction medium, wherein a water-soluble manganese complex is used as oxidation catalyst, wherein a terminal olefin is used with a limited solubility at 20° C. of at least 0.01 to 100 g in 1 liter water, and wherein the molar ratio of terminal olefin to hydrogen peroxide is in the range of from 1:0.1 to 1:2.

MODE(S) FOR CARRYING OUT THE INVENTION

As used in the current specification, the expressions epoxidation and oxidation refer to the same reaction; the conversion of a carbon-carbon double bond into an oxirane ring. Oxidation and epoxidation may also result in the preparation of diols and other derivatives, for instance in case of bleaching, but such is considered undesirable in the context of the present invention.

The invention is hereafter discussed in greater detail.

In terms of water-soluble manganese complexes that may be used as oxidation catalyst, many suitable complexes are known. Typically the catalyst comprises a manganese atom or a number of manganese atoms coordinated with a ligand or ligands. The manganese atom(s) may be in a II, III or IV oxidation state and be activated during the reaction. Of particular interest are binuclear manganese complexes, such as those described in the open and patent literature described in the introductory part of this patent application. Suitable manganese complexes therefore include mononuclear species of the general formula (I): [LMnX₃]Y  (I) and binuclear species of the general formula (II): [LMn(μ-X)₃MnL]Y₂  (II) wherein Mn is a manganese; L or each L independently is a polydentate ligand, preferably a cyclic or acyclic compound containing 3 nitrogen atoms; each X independently is a coordinating species and each μ-X independently is a bridging coordinating species, selected from the group consisting of: RO⁻, Cl⁻, Br⁻, I⁻, F⁻, NCS⁻, N₃ ⁻, I₃ ⁻, NH₃, NR₃, RCOO⁻, RSO₃ ⁻, RSO₄ ⁻, OH⁻, O²⁻, O₂ ²⁻, HOO⁻, H₂O, SH⁻, CN⁻, OCN⁻, and S₄ ²⁻ and combinations thereof, wherein R is a C₁-C₂₀ radical selected from the group consisting of alkyl, cycloalkyl, aryl, benzyl and combinations thereof, and Y is an oxidatively-stable counterion. Counterion Y may for instance be an anion selected from the group consisting of RO⁻, Cl⁻, Br⁻, I⁻, F⁻, SO₄ ²⁻, RCOO⁻, PF₆ ⁻, acetate, tosylate, triflate (CF₃SO₃ ⁻) and a combination thereof with R once again being a C₁ to C₂₀ radical selected from the group consisting of alkyl, cycloalkyl, aryl, benzyl and combinations thereof. The type of anion is not very critical, although some anions are more preferred than others. A preferred counterion is PF₆ ⁻. Ligands which are suitable for the present invention are acyclic compounds containing at least 7 atoms in the backbone or cyclic compounds containing at least 9 atoms in the ring, each having the nitrogen atoms separated by at least two carbon atoms. A preferred class of ligands is that based on (substituted) triazacyclononane (“Tacn”). The preferred ligand is 1,4,7-trimethyl-1,4,7,-triazacyclononane (“TmTacn”), which is commercially available from, for instance, Aldrich. In this respect it is important to note that the water-solubility of the manganese catalyst is a function of all the aforementioned catalyst components. For instance, a mononuclear manganese complex prepared from MNSO4 and TmTacn was found to be insufficiently soluble.

Dinuclear manganese complexes are preferred, because of their greater activity and solubility in water. Preferred dinuclear manganese complexes are those of the formula [Mn^(IV) ₂(μ-O)₃L₂]Y₂, wherein L and Y have the meaning identified above, preferably TmTacn as ligand, and PF₆ ⁻ or acetate (CH₃CO₂ ⁻, hereinafter OAc) as counterion.

According to the present invention, the manganese complex may be utilized directly or as absorbed onto a solvent insoluble support surface. Illustrative but nonlimiting examples of such substrates are structured aluminosilicates (e.g. Zeolite A, faujasite and sodalite), amorphous aluminosilicates, silica, alumina, charcoal, microporous polymeric resins (e.g. polystyrene beads formed through high internal phase emulsion technology) and clays (especially layered clays such as hectorite and hydrotalcite). Relative weight ratios of the manganese complex to the support may range anywhere from about 10:1 to about 1:10,000.

The manganese complex is used in catalytically effective amounts. Typically, the catalyst is used in a molar ratio of catalyst (Mn) versus the terminal olefin of from 1:10 to 1:10,000,000, preferably of from 1:20 to 1:100,000, most preferably of from 1:50 to 1:1000. As a matter of convenience the amount of catalyst may also be expressed in terms of its concentration, when keeping in mind the volume of the aqueous medium. For instance, it may be used in a molar concentration (based on the Mn) of from 0.001 to 10 mmol/L, preferred of from 0.01 to 7 mmol/L and most preferably of from 0.01 to 2 mmol/L. In this respect it is also important to note that the epoxidation is first order on the catalyst concentration and proportional to the catalyst amount. With increase in the catalyst amount, the activity increases. The higher amounts, however, need to be balanced by the higher cost.

The aqueous reaction medium typically is a water phase containing the dissolved epoxide and/or terminal olefin and less than 25% by volume, preferably only minor amounts, if any of other organic compounds. Although not preferred, the reaction medium may contain minor amounts of co-solvents such as methanol and acetone and the like. Whilst excluding the presence of the epoxide and/or terminal olefin, the aqueous reaction medium suitably comprises at least 90% by volume of water, preferably 95% v, more preferably 99% v, still more preferably 99.9% v of water. Most preferably, however, the aqueous reaction medium is essentially a 100% water phase.

The aqueous reaction medium may contain a buffer system so as to stabilize the pH. For instance, it has been found that the aqueous reaction medium is suitably stabilized in a pH range of 2.5 to 8, whereas the preferred pH range is between 3 and 7 and the most preferred is between 3.5 to 6.5. The pH is therefore (well) below that used when bleaching olefins, typically carried out at more alkaline conditions (e.g., pH adjusted with NaHCO₃ to 9.0). The suitable or preferred range may be achieved by several known acid-salt combinations, with the preferred combination being based on oxalic acid-oxalate salt. When oxalic acid and sodium oxalate are used, the pH ratio may be varied from 3.7 to 4.2. Typically, this buffer may be used in a molar ratio to the catalyst of about 10:1, but the amounts may be varied broadly, e.g., ranging from 1:1 to 100:1.

The aqueous reaction medium may also contain a phase transfer agent and/or a surfactant, in particular if a terminal olefin is used with low solubility (e.g., below 0.1 g/L water). Known phase transfer agents that may be used in the process of the invention include quaternary alkyl ammonium salts. Known surfactants that may be used in the process of the invention include non ionic surfactants such as Triton X100™ available from Union Carbide.

The reaction conditions for the catalytic oxidation may be quickly determined by a person skilled in the art. Pressure is not of particular relevance. The reaction is exothermic, and cooling of the reaction medium may be required. The reaction is preferably carried out at temperatures anywhere from −5° C. to 30° C., preferably from 0° C. to 20° C., and most preferably from 0° C. to 10° C.

Of particular importance in the process of the current invention is that the process is carried out in a biphasic system, which definition includes multiphasic systems in case the 1,2-epoxide and the terminal olefin form separate phases. Because the reaction is carried out in a biphasic system, using a terminal olefin with a limited solubility as defined hereinafter, moreover at the right molar ratio of hydrogen peroxide versus terminal olefin, the inventors have achieved producing the corresponding 1,2-epoxide at high turnover numbers, with high selectivity towards the 1,2-epoxide with moreover improved ease of isolating the produced 1,2-epoxide. The biphasic system is created by adding the terminal olefin (as reactant) in an amount greater than what dissolves in the reaction medium. The biphasic system may also be created by conversion of the terminal olefin into the corresponding 1,2-epoxide, which then separates from the reaction medium and forms the organic phase. To ensure optimal results, the addition of reactants should be to the aqueous medium and in case of mixing, back-mixing of the produced 1,2-epoxide should preferably be avoided, if possible. By way of example, the conversion of allyl chloride (“AC”) into epichlorohydrin is discussed hereinafter, which in fact may result in a three layer system comprising an organic phase at the bottom, believed to be rich in ECH, whereas it also comprises an organic phase on top that is rich in the starting allyl chloride. In this case the mixing or stirring of the system should preferably be such as to leave the bottom layer substantially undisturbed.

Once again, to have the reaction carried out in a biphasic system, the terminal olefin should have at most limited solubility in the aqueous reaction medium. Outside the scope of the current invention are therefore 4-vinylbenzoic acid, styrylacetic acid, trans-3 or trans-2-hexenoic acid or allyl alcohol as used in the aforementioned EP0618202, since they all are soluble in water. Quite surprisingly, the current inventors actually found a greater production of 1,2-epoxide at higher turnover numbers when using allyl chloride or allyl acetate as compared to allyl alcohol, even though the former have only limited solubility, whereas the latter is fully miscible with water. On the other hand, some solubility is required; conversion of unsubstituted α-olefins (like 1-octene) cannot be achieved by the process of the current invention. Suitable terminal olefins hence have a solubility (expressed in grams per liter water at 20° C.) in the range of from 0.01 to 100 g/L, more preferably from 0.1 to 50 g/L, most preferably from 0.5 to 20 g/L. Examples of suitable terminal olefins include halogenated olefins having from 3 to 8 carbon atoms in the molecule, hydroxyl-substituted olefins having 4 to 6 carbon atoms in the molecule, carbonyl-substituted olefins having 3 to 6 carbon atoms in the molecule, alkoxy-substituted olefins having 3 to 8 carbon atoms in the molecule, alkenoic acids having 7 to 8 carbon atoms and esters of alkenoic acids having in total 4 to 8 carbon atoms, allyl esters of alkanoic acids having 3 to 8 carbon atoms, etc. Of particular (commercial) relevance are allyl bromide (solubility of 4 g/L), allyl chloride (solubility of 3.6 g/L), and allyl acetate (solubility of about 10 g/l). Also suitable and of approximately the same solubility are allyl propionate, allyl butanoate, allyl hexanoate, allyl octanoate, allyl decanoate, allyl stearate, allyl palmitate, allyl salicylate, allyl lactate, and allyl succinate. Preferred terminal olefins are allyl chloride (because of the commercial interest and ease of isolating the product, as discussed hereinafter) and allyl acetate. In addition to the mono-olefins mentioned above, also di-olefins such as for instance diallyl glutarate, diallyl adipate, diallyl pimelate, diallyl oxalate, diallyl maleate, diallyl phthalate and diallyl isophthalate may be used.

The catalytic oxidation of the present invention is carried out using hydrogen peroxide as oxidant. Other oxidants may be used, i.e. as precursor to the hydrogen peroxide, but given the availability and to reduce environmental impact hydrogen peroxide is the preferred oxidant. Hydrogen peroxide has strong oxidizing properties. As bleaching agent it is mostly used for bleaching paper. It is typically used in an aqueous solution. The concentration of hydrogen peroxide may vary, from 15% (e.g, consumer grade for bleaching hair) to 98% (propellant grade), with a preference for industrial grades varying from 20 to 60%, preferably from 30 to 50%.

The molar ratio of terminal olefin to hydrogen peroxide is very important in the process of the current invention. If too much hydrogen peroxide is used, then the selectivity towards the 1,2-epoxide reduces due to the production of undesirable side-products. If not enough hydrogen peroxide is used, then the turnover number is suboptimal. This is therefore significantly different from bleaching conditions described in the prior art, where excessive amounts of hydrogen peroxide are used. The molar ratio of terminal olefin to hydrogen peroxide is in the range of from 1:0.1 to 1:2, more preferably from in the range of from 0.5:1 to 1.2:1 and most preferably about 1:1. To ensure optimal peroxide efficiency, the hydrogen peroxide is preferably added to the aqueous reaction medium at a rate about equal to the reaction rate of the catalytic oxidation.

The catalytic oxidation may be performed in a batch process, in a continuous process or in a semi-continuous process. Indeed, the process may be modified in various aspects without departing from the gist of the invention.

By way of general example the catalytic oxidation of allyl chloride is described hereafter.

The catalytic oxidation may be performed in a common continuous stirred tank reactor, with means of stirring provided extending, for instance, from the top partway to the bottom, leaving a bottom zone which will contain the organic phase rich in ECH, mostly undisturbed. For instance, this may be an elevated, common blade agitator operating under an agitation speed of around 250 rpm in a batch reactor. The catalyst, aqueous reaction medium and reactants may be added in batch, or the reactants may be added over a period of time. As a result of the process of this invention, ECH is formed as a separate bottom layer, which can be removed with ease either at the end of the (bath) reaction or continuously. If hydrogen peroxide is added during the reaction, then it is added to either the (stirred) organic phase comprising the allyl chloride or the (stirred) aqueous reaction media.

In (semi)continuous operations, various recycling streams may be used to control the reaction conditions (maintained at a temperature of between −5° C. and 10° C.) and to optimize the production rate.

In terms of process design, a settler may be added to optimize the gravitational separation of the ECH. Likewise, a membrane unit may be used to recycle the aqueous reaction medium with reduced loss of catalyst.

On example of a mass balance for the reaction process according to the invention is:

ECH about 11 000 kg/h

AC about 9 100 kg/h

H₂O₂(35%) about 6 457 kg/h

H₂O about 2 140 kg/h

As a result of this mass balance, the ratio ECH/cat is about 8000 mol/mol.

The following examples will more fully illustrate selected embodiments of this invention. All parts, percentages and proportions referred to herein and in the appended claims are by weight unless otherwise indicated.

EXAMPLES Example 1

The catalytic oxidation was carried out with a catalyst of the formula:

Also used is an oxalate/oxalic acid buffer, with 35% aqueous H₂O₂ as oxidant, and water as aqueous reaction medium. The experiment is carried out with allyl chloride as the terminal olefin.

Experimental:

In a typical epoxidation reaction 0.0093 mmol of catalyst in 50 mL of water, 112.5 mot of sodium oxalate in 7.5 mL of H₂O and 112.5 μmol of oxalic acid in 7.5 mL of H₂O were taken into a three-neck round-bottomed flask equipped with a mechanical stirrer. The reaction started with the addition of olefin (150 mmol) and dilute H₂O₂ (200 mmol) at 4° C.

10 mL of extra water was added as solvent for the reaction. The oxidant was added under flow conditions with 8.8 mL/hr into the reaction solution. The pH of the reaction solution was 3.5 to 3.6 and the stirring rate was maintained at 210 rpm for the most of the experiments with mechanical stirrer.

Results and Discussion

The manganese complex produced ECH efficiently using water as solvent. During the epoxidation using water as solvent, at the beginning of the reaction, AC is present as a separate layer on top of the aqueous catalyst solution. As the epoxidation progressed the ECH (having a higher density) separated at the bottom along with some AC dissolved in it. The reaction system thus formed three phases from top to bottom, organic (mainly AC), an aqueous and a second organic (mainly ECH) phase. At the end of the reaction both the top and bottom organic fractions constituted major amounts of ECH and AC. Minor amounts of AC and ECH were also found in the aqueous fraction.

This example provided a 50% yield of epoxide based on olefin produced at 40% selectivity of peroxide, with 7800 TON. There were no noticeable amounts of diols or other side products produced.

Example 2

Various experiments were carried out in the manner of Example 1. In Table 1 the results of the epoxidation of AC at various stirring rates are presented.

TABLE 1 Epoxidation of AC: Variation of stirring rate Time Stirring rate ECH TON No. period (h) (rp--m) (mmol) (for ECH) 1 6 650 33 3500 2 6 500 36 3900 3 6 210 73 7800 4 4 210 64 6900 5 4 100 37 3900

This example illustrates that the yield of epoxide increases with the stirring rate until the bottom layer become disturbed.

Example 3 Epoxidation of Various Olefins

Epoxidation reactions of various olefins performed with the above manganese complex have been carried out in the manner described in Example 1. The results are shown in Table 2.

TABLE 2 Epoxidation of various olefins Solubility Time Olefin in water period epoxide No (mmol) (g/L) (h) (mmol) TON 1 Allyl alcohol miscible 8 53 5700 2 Allyl chloride 3.6 8 76 8100 3 Allyl acetate ~10 8 137 14500 4 1-octene 2.7 × 10⁻⁴ 8 traces —

This example illustrates that the yield of epoxide and the turnover number increases as a result of solubility, provided the solubility remains limited. Experiment Nos. 1 and 4 are comparative.

Example 4 Variation in Catalyst Amount

Epoxidation of allyl acetate was carried out in the manner of Example 1, however, with a variation in catalyst amount. This example illustrates that increased amounts of catalyst leads to increased production of epoxides; hence it is possible to decrease the time period. In the best experiment, allyl acetate was converted at 92% yield into glycidyl acetate (GlAc) in 0.5 hours at 95% efficiency. The results are included in the following Table.

TABLE 3 Epoxidation of allyl acetate: Variation of catalyst amount Time Catalyst amount Efficiency GlAc No. period (h) (mmol) peroxide (%) (mmol) TON 1 8  9.4 × 10⁻³ nd 137 14500 2 4  9.4 × 10⁻³ 92 122 13000 3 2 18.3 × 10⁻³ 99 126 6800 4* 1 36.7 × 10⁻³ 91 126 3433 5* 0.5 73.4 × 10⁻³ 95 138 1880 *olefin:hydrogen peroxide ratio was 1:1.03

Example 5 Effect of pH

In the previous experiments the epoxidation reactions have been performed at low pH around 3.5 to 3.6. Here we show that the catalyst is active in both acidic and basic conditions, that is at pH=2.6 with only oxalic acid present, as well as at pH=8 with only sodium oxalate. These results give evidence that the catalyst system is active in the wide pH range for AC epoxidation.

TABLE 4 Effect pH for epoxidation of allyl chloride peroxide mmol of ECH formed consumed in Organic in Aqueous TON Selectivity of No. pH (mmol) phase phase ECH peroxide (%) 1 2.6 55 15.4 7.6 2400 42 2 8 121 29 19 5000 39

Example 6 Effect of the Counterion

In the previous experiments the epoxidation reactions have been carried out with a catalyst having PF6<″> as counterion. In this experiment the corresponding [Mn₂(μ-0)₃TmTacn₂](OAc)₂ has been used. The catalyst is quite active, albeit that it was found that a double amount of oxalate/oxalic acid buffer was required to produce similar activity to that of the PF₆ salt. A preliminary result of the use of this catalyst is shown in Table 5.

TABLE 5 Epoxidation of allyl chloride with [Mn₂O₃L₂](OAc)₂ Time Stirring rate ECH No. period (h) (rpm) (mmol) TON 1 8 1000 674 3100 

The invention claimed is:
 1. A process for the manufacture of a 1,2-epoxide, comprising: reacting a terminal olefin with hydrogen peroxide in the presence of a catalyst, in a biphasic system comprising an organic phase and an aqueous reaction medium, and wherein the molar ratio of the terminal olefin to the hydrogen peroxide is in the range of from 1:0.1 to 1:1, and wherein the catalyst comprises a water-soluble manganese complex of a mononuclear manganese complex of the formula (I): [LMnX₃]Y  (I) or a binuclear manganese complex of the formula (II): [LMn(μ-X)₃MnL]Y₂  (II) wherein Mn is a manganese atom; L or each L independently is a polydentate ligand of triazacyclononane or 1,4,7-trimethyl-1,4,7,-triazacyclononane; each X independently is a coordinating species selected from the group consisting of: RO⁻, Cl⁻, Br⁻, I⁻, F⁻, NCS⁻, N₃ ⁻, I₃ ⁻, NH₃, NR₃, RCOO⁻, RSO₃ ⁻, RSO₄ ⁻, OH⁻, O²⁻, O₂ ²⁻, HOO⁻, H₂O, SH⁻, CN⁻, OCN⁻, and S₄ ²⁻ and combinations thereof, wherein R is selected from the group consisting of C₁-C₂₀ alkyl, C₁-C₂₀ cycloalkyl, C₁-C₂₀ aryl, benzyl and combinations thereof and each μ-X independently is a bridging coordinating species selected from the group consisting of: RO⁻, Cl⁻, Br⁻, F⁻, F⁻, NCS⁻, N₃ ⁻, I₃ ⁻, NH₃, NR₃, RCOO⁻, RSO₃ ⁻, RSO₄ ⁻, OH⁻, O²⁻, O₂ ²⁻, HOO⁻, H₂O, SH⁻, CN⁻, OCN⁻, and S₄ ²⁻ and combinations thereof, wherein R is selected from the group consisting of C₁-C₂₀ alkyl, C_(r) C₂₀ cycloalkyl, C₁-C₂₀ aryl, benzyl and combinations thereof, and Y is an anion counterion is selected from the group consisting of RO⁻, Cl⁻, Br⁻, I⁻, F⁻, SO₄ ²⁻, RCOO⁻, PF₆ ⁻, acetate, tosylate, triflate (CF₃SO₃ ⁻) and a combination thereof, wherein R is selected from the group consisting of C₁-C₂₀ alkyl, C₁-C₂₀ cycloalkyl, C₁-C₂₀ aryl, benzyl and combinations thereof, wherein the aqueous reaction medium further comprises a buffer system to stabilize a pH, and the aqueous reaction medium has a pH range from 3 to 6.5.
 2. The process of claim 1, further comprising stirring the biphasic system.
 3. The process of claim 2, wherein the stirring the biphasic system comprises stirring the system with a stirrer at between 100 rpms and 650 rpm.
 4. The process of claim 1, wherein the aqueous reaction medium further comprises a buffer system at a buffer to catalyst ratio from 10:1 to 100:1.
 5. The process of claim 4, wherein the buffer system comprises an acid-salt combination.
 6. The process of claim 1, wherein the catalyst is present in a concentration from 0.01 mmol/L to 10 mmol/L.
 7. The process of claim 1, wherein the catalyst is used in a molar ratio of the catalyst (Mn) to the terminal olefin of from 1:10 to 1:10,000,000.
 8. The process of claim 1, wherein the terminal olefin is one or more terminal olefins having a solubility in the range of from 0.1 to 50 g/L.
 9. The process of claim 1, wherein the biphasic system is created by adding the terminal olefin in an amount greater than what dissolves in the reaction medium, by conversion of the terminal olefin into the corresponding 1,2-epoxide, or combinations thereof.
 10. The process of claim 1, wherein the biphasic system further includes a phase transfer agent, a surfactant, or both.
 11. The process of claim 1, wherein the catalyst comprises a binuclear manganese complex of the formula (II): [LMn(μ-X)₃MnL]Y₂  (II), wherein Mn is a manganese; L or each L independently is a polydentate ligand of triazacyclononane or 1,4,7-trimethyl-1,4,7,-triazacyclononane; each μ-X independently is a bridging coordinating species of: O²⁻, RCOO⁻, RSO₃ ⁻, RSO₄ ⁻, wherein R is selected from the group consisting of C₁-C₂₀ alkyl, C₁-C₂₀ cycloalkyl, C₁-C₂₀ aryl, benzyl and combinations thereof, and Y is selected from the group consisting of SO₄ ²⁻, PF₆ ⁻, acetate, and combinations thereof.
 12. The process of claim 1, wherein the molar ratio of the terminal olefin to the hydrogen peroxide in the range of from 1:0.1 to 1.2:1.
 13. The process of claim 1, wherein the reaction is performed in a batch process, in a continuous process or in a semi-continuous process.
 14. The process of claim 1, wherein the aqueous reaction medium comprises a 100% aqueous medium excluding any dissolved epoxide and terminal olefin.
 15. The process of claim 8, wherein the aqueous reaction medium comprises a pH in the range of from 3 to 4.2.
 16. The process of claim 1, wherein the catalyst comprises a binuclear manganese complex of the formula (II): [LMn(μ-X)₃MnL]Y₂  (II), wherein Mn is a manganese; L or each L independently is a polydentate ligand of triazacyclononane or 1,4,7-trimethyl-1,4,7,-triazacyclononane; each μ-X independently is a bridging coordinating species of: O²⁻, RCOO⁻, RSO₃ ⁻, RSO₄ ⁻, wherein R is selected from the group consisting of C₁-C₂₀ alkyl, C₁-C₂₀ cycloalkyl, C₁-C₂₀ aryl, benzyl and combinations thereof, and Y is selected from the group consisting of SO₄ ²⁻, PF₆ ⁻, acetate, and a combination thereof; wherein the aqueous reaction medium further comprises a buffer system with a pH range from 3.0 to 4.2; and wherein the molar ratio of the terminal olefin to the hydrogen peroxide in the range of from 1:0.1 to 1.2:1.
 17. The process of claim 1, wherein the terminal olefin is selected from the group of halogenated olefins having from 3 to 8 carbon atoms in the molecule, hydroxyl-substituted olefins having 4 to 6 carbon atoms in the molecule, carbonyl-substituted olefins having 3 to 6 carbon atoms in the molecule, alkoxy-substituted olefins having 3 to 8 carbon atoms in the molecule, alkenoic acids having 7 to 8 carbon atoms and esters of alkenoic acids having in total 4 to 8 carbon atoms, and allyl esters of alkanoic acids having 3 to 8 carbon atoms.
 18. The process of claim 17, wherein the terminal olefin is selected from the group of allyl bromide, allyl chloride, allyl acetate, allyl propionate, allyl butanoate, allyl hexanoate, allyl octanoate, allyl decanoate, allyl stearate, allyl palmitate, allyl salicylate, allyl lactate, allyl succinate, diallyl glutarate, diallyl adipate, diallyl pimelate, diallyl oxalate, diallyl maleate, diallyl phthalate, and diallyl isophthalate.
 19. The process of claim 17, wherein the terminal olefin is one or more terminal olefins selected from the group of halogenated terminal olefins having from 3 to 8 carbon atoms in the molecule, alkenoic acids having 7 to 8 carbon atoms and esters of alkenoic acids having in total 4 to 8 carbon atoms, and allyl esters of alkanoic acids having 3 to 8 carbon atoms.
 20. The process of claim 5, wherein the acid-salt combination comprises oxalic acid-oxalate salt. 